Hydrocracking of heavy oil and residuum with a dispersing-type catalyst

ABSTRACT

This invention discloses a dispersing-type catalyst for catalytic  hydrocring of heavy oil and residuum, the preparation method thereof and a suspension bed hydrocracking process for hydrocracking of heavy oil and residuum using said catalyst. Said catalyst comprises 2 to 15 wt % Mo, 0.1 to 2 wt % Ni and 0.1-3 wt % P. The preparation method comprises dissolving oxides or salts of metals such as Mo, Ni in water. The process comprises mixing the heavy oil and residuum feedstock with the catalyst, heating the mixture and introducing the mixture into a suspension bed reactor, performing the hydrocracking reaction at 380-460° C. under 10-15 MPa of hydrogen pressure, in which the catalyst is added in an amount to provide 150-150O ppm active metals. The yield of light oil according to the process is more than 70 wt %, substantially without coking.

This is a division of application Ser. No. 08/754,877 filed on Nov. 22,1996, now U.S. Pat. No. 5,948,721.

FIELD OF THE INVENTION

The present invention relates to a dispersing-type catalyst forcatalytic hydrocracking of heavy oil and residuum, a method forpreparing the same and the use thereof in catalytic hydrocracking ofheavy oil and residuum.

BACKGROUND OF THE INVENTION

Hydroconversion process of heavy oil and residuum is one of the mainprocesses for converting a heavy hydrocarbonaceous feedstock to lowerboiling products. Generally heterogeneous catalyst, such as alumina orsilica-alumina supported sulfide of cobalt, molybdenum or nickel, isused in the process. The constituents having higher molecular weight inheavy oil and residuum deposit on the surface of the catalyst, block thepores of the catalyst, and then result in rapid decline of thehydrogenation activity. Eventually coke and metal impurities removedfrom heavy oil and residuum deposit on the surface of the catalyst andresult in deactivation of the catalyst. Moreover, the rapid increase inpressure drop of the bed layer makes it difficult to maintain normaloperation, which becomes more serious when the feedstock contains highermetal and carbon residue, thereby, the catalyst displays short servicelife and bad operation stability, therefore shut-down is more frequent.

In order to solve these problems, many dispersing-type catalyst havebeen proposed. Chinese Patent Application CN 1035836A discloses adispersing-type catalyst and its preparation method, wherein ironcompound (especially ferrous sulfate) is ground with coal powder in oilto form an iron-coal slurried catalyst. Subsequently, the catalyst ismixed with heavy oil to form feedstock for hydrogenation reaction.

The catalyst can be substantially dispersed into heavy oil. However,metal iron has only a little hydrogenation activity and coking isserious in the reaction process. Otherwise, the coal added as catalystbecomes coking support in the process, resulting in a lot ofoil-insoluble solids in the product, thus, it brings much difficulty inseparation and after-treatment, besides, the solid particles also wearthe pipes and device.

U.S. Pat. No. 4,637,870 discloses a hydroconversion process, whereinphosphoric acid is added to an aqueous solution of phosphomolybdic acid.The phosphoric acid-phosphomolybdic acid aqueous solution is mixed witha hydrocarbonaceous material to form a catalyst precursor concentrate.The precursor concentrate is dehydrated, vulcanized, then mixed withheavy oil and residuum feedstock and introduced into a reactor toperform hydrogenation reaction. In the patent, it is mentioned thatcommercially available phosphomolybdic acid typically contains an atomicratio of P/Mo ranging from about 0.08:1 to 0.01:1. If the phosphoricacid is added to the phosphomolybdic acid in an amount to provide anatomic ratio of P/Mo in the solution ranging from 0.12:1 to 0.45:1,coking can be obviously decreased (as shown in the examples, from 5.06%to 1.78%). In practice, however, this level of coking is still too high.Moreover, it is very inconvenient to premix the catalyst withhydrocarbonaceous material and predehydrate the catalyst beforeintroducing it into a reactor in practical operation.

U.S. Pat. No. 4,637,871 discloses a hydrocoversion process utilizing anaqueous solution of phosphomolybdic acid as catalyst In this process,the aqueous solution of phosphomolybdic acid must comprise less than 5wt % molybdenum. If the content is higher than 5 wt %, coking willremarkably increase. The speed and degree of hydrogenation reactiondepend on the concentration of active metals in the reaction system. Ifan aqueous solution of phosphomolybdic acid having low concentration isused, a lot of water will be introduced into the catalyst-oil system inorder to reach a proper concentration of active metals in the reactionsystem.

U.S. Pat. No. 5,039,392 discloses another modified process on the basisof the two patent process mentioned above, in which element sulfur isused as a vulcanizing agent to vulcanize the catalyst precursorconcentrate, in order to simplify the preparation of the precursorconcentrate. But, the following steps are still necessary: dispersingthe aqueous solution of the catalyst into hydrocarbonaceous material,dehydrating, vulcanzing, adding it into feedstock and introducing into areactor to perform the reaction. It is mentioned in the description thatthe amount of catalyst used is in the range of 50 to 300 ppm, however,an amount of 208 ppm is used in every example. In all examples, cokeyields (solid product yield) are about 2.0 wt %, at least 1.8 wt %.Obviously, it is too high to be acceptable in practical operation.

High coke yield is a common problem in other similar techniques.therefore, it is necessary to propose a new technique to further lowerthe coke yield in catalytic hydrogenation of heavy oil and residuum.

In order to overcome these problems, the inventors have concentratedtheir research on the development of a catalyst which can furtherdecrease the coke yield in catalytic hydrocracking of heavy oil andresiduum, and has no disadvantagous effect on producing lower boilingproducts in the hydrocracking reaction.

SUMMARY OF THE INVENTION

The object of the present invention is to provide a dispersing-typecatalyst for catalytic hydrocracking of heavy oil and residuum, whichcomprises 2 to 15 wt % Mo, 0.1 to 2 wt % Ni and 0.1 to 3 wt % P.

Another object of the present invention is to provide a method forpreparing said dispersing-type catalyst, which comprises dissolvingoxides or salts of transition metals such as Mo, Ni in water to form anaqueous solution.

Still another object of the present invention is to provide a suspensionbed catalytic hydrocracking process for heavy oil and residuum, whichcomprises mixing heavy oil and residuum feedstock with the catalystaccording to the present invention, heating the mixture, introducing themixture into a suspension bed reactor, and performing the hydrocrackingreaction at 380-460° C. under 10-15 MPa of hydrogen pressure, in whichthe catalyst is added in an amount to provide from 150 to 1500 ppmactive metals.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a flow chart of one embodiment of the catalytic hydrocrackingprocess of the present invention for heavy oil and residuum.

FIG. 2 is a flow chart of one embodiment of catalytic hydrocrackingprocess of the present invention for heavy oil and residuum, in whichthe temperature of the feedstock is very high.

DETAILED DESCRIPTION OF THE INVENTION

The catalyst provided by the present invention for catalytichydrocracking of heavy oil and residuum is an aqueous solution, whichcan uniformly disperse into heavy oil and residuum feedstock and form anemulsion. Element nickel is introduced into Mo/P system in the catalystof the present invention so as to increases hydrogenation activity ofthe catalyst and effectively decrease coking in the reaction process.The concentration of molybdenum in the catalyst of the present inventionmay be higher than 5 wt %, unlike the prior art disclosed in U.S. Pat.No. 4,637,871 (less than 5 wt %), without resulting in the increase ofcoking in the reaction process. This is accomplished by introducingnickel and then adjusting the composition of water-soluble catalyst.Increasing the contents of active metals in the catalyst would lower thecost of equipment and operation and reduce the quantity of waste.

In accordance with the invention, the dispersing-type catalyst forcatalytic hydrocracking of heavy oil and residuum comprises 2 to 15 wt %Mo, 0.1 to 2 wt % Ni and 0.1 to 3 wt % P. The catalyst may compriseother elements, provided that they have no reverse effect on theproperty of the catalyst.

Preferably, the catalyst comprises 5 to 10 wt % Mo, 0.1 to 1.0 wt % Niand 0.2 to 1 wt % P.

Most preferably, the catalyst comprises 6 to 8 wt % Mo, 0.3 to 0.8 wt %Ni and 0.2 to 0.4 wt % P.

The catalyst of the present invention can be prepared by dissolving thecompounds or salts of transition metals such as Mo, Ni in water.

Preferably, the catalyst can be prepared by dissolving the oxides orsalts of said metals in an aqueous solution of an acid.

The said acid may be common acids used in the art, and phosphoric acidis preferred.

The oxides or salts of Mo and Ni may be, for example, molybdenum oxide,phosphomolybdic acid, nickel carbonate, nickel oxide and the like, amongwhich molybdenum oxide, phosphomolybdic acid, nickel carbonate or nickelacetate is preferred, molybdenum oxide and basic nickel carbonate aremore preferred.

The method for preparing the catalyst of the present invention, forexample, may comprise: adding a predetermined amount of phosphomolybdicacid and nickel nitrate to water in proper amounts, and dissolving themcompletely, optionally by heating to accelerate the dissolution, toobtain an aqueous catalyst solution; or adding a predetermined amount ofmolybdenum oxide and basic nickel carbonate to aqueous phosphoric acidsolution which contains 0.2-3 wt % P, and dissolving them completely,optionally by heating to accelerate the dissolution, to obtain anaqueous catalyst solution.

As mentioned above, the catalyst of the present invention can be used incatalytic hydrocracking of heavy oil and residuum, and an unpredictedand remarkable effect can be achieved. According to the suspension bedcatalytic hydrocracking process of the present invention, the catalystcan be highly dispersed into heavy oil and residuum, and then thehydrocracking reaction can be performed in a reactor which has no fixedcatalyst bed. The method can convert a large quantity of heavy oil andresiduum into lower boiling fractions. The adding of the catalyst andcontrol of the reaction are facilitated in operation, and the desiredyield of conversion to lower boiling products is fulfilled and the cokeyield in the reaction process can be lowered to less than 1.0%, or evenless than that Moreover, according the process of the present invention,desirable products can be obtained to meet the market demand or meet therequirement of upstream and/or downstream flows, by adjusting the metalconcentrations, element ratios in the catalyst and other reactionconditions to achieve the desired distribution of products in thecracker unit, in which a major amount of the products have the desiredboiling range.

According to the process of the present invention, the catalyst is addedinto heavy oil and residuum feedstock conventionally and economically tocarry out the hydrocracking reaction in a reactor.

The process of the present invention comprises mixing the catalyst ofthe present invention with a heavy oil and residuum feedstock, heatingthe mixture, introducing the mixture into a suspension bed reactor andperforming the hydrocracking reaction at 380-460° C. under 10-15 MPa ofhydrogen pressure; wherein the catalyst is added in an amount to providefrom 150 to 1500 ppm active metals.

In one embodiment of the hydrocracking process of the present invention,heavy oil and residuum feedstock is mixed directly with the catalyst,and then the resulting mixture is introduced into the reaction zone toperform hydrocracking reaction. There is no need to prepare a catalystprecursor.

In another embodiment of the hydrocracking process of the presentinvention, the feedstock which is cold is mixed directly with thecatalyst, then mixed with hydrogen, the resulting mixture is heated in aheating oven and then enters the reactor.

In still another embodiment of the hydrocracking process of the presentinvention, the feedstock having higher temperature comes from upstreamdevice, and the catalyst is injected into hot oil line by a pump via adistributor, subsequently, the resulting mixture is introduced into thereaction system.

In still another embodiment of the hydrocracking process of the presentinvention, when the feedstock is about 100° C. and has high viscosity,not suitable for mixing with the catalyst directly, the catalyst isfirst premixed with a small amount of heavy oil and residuum having lowviscosity, and then mixed with the feedstock having high viscosity, oradded into heavy oil and residuum feedstock having high viscosity by adistributor.

In order to meet the market demand or the requirement of productdistribution in the device, desirable products can be obtained byadjusting the contents of metal Mo, Ni and element P in the catalyst andother reaction conditions.

The catalyst used in the hydrocracking process of the present inventionfor a heavy oil and residuum feedstock is the catalyst of the presentinvention.

In the heavy oil and residuum hydrocracking process of the presentinvention, the catalyst is added in an amount to provide preferably200-1000 ppm active metals.

The hydrocracking process of the present invention will be described inmore detail below referring to the figures. It must be understood thatthe present invention is not limited to the embodiments described belowin any way, which only describe the process of the present invention.

Referring to FIG. 1, a heavy oil and residuum feedstock and the catalystare introduced separately by lines 1 and 2 into mixing device 3. Saidmixing device 3 is a stirring tank, colloid mill, static mixer or thelike. The feedstock and the catalyst are mixed uniformly in the mixingdevice. If the viscosity of the feedstock is so high that it isdifficult to mix by common method at a temperature below 100° C., thecatalyst may first be mixed with a small amount of heavy oil andresiduum at normal pressure and then mixed with the feedstock havinghigh viscosity. The mixed feedstock is passed by line 4, pump 5 and line7 to heater 8. Hydrogen is introduced into the system by line 6. Thefeedstock is heated to 360-390° C. in heating oven 8, and then passed byline 9 to reactor 10. The operating conditions in the reactor are:Hydrogen pressure 10-18 MPa, hourly space velocity of feedstock liquid0.5-2 h⁻¹, reaction temperature 390-460° C., hydrogen/oil ratio 500-1500(volume ratio). The reaction products are passed by line 11 tohigh-pressure separator 12. The separated gases is passed by line 17 togas recovery and separating system 18. Hydrogen is washed, purified andrecycled to the reactor by line 19. Lighter oil is withdrawn by line 20.The liquid material separated from high-pressure separator 12 is passedby line 13 to a solid separation device 14. Solids can be separated byfiltration or centrifugal separator. The liquid product from whichcatalyst powder and coke formed have been removed is withdrawn by line16. The filtrated solid material may be recycled to a reactor or metalrecycling system.

When the temperature of feedstock is high (for example the heavy oil andresiduum comes from upstream device) and not suitable for mixing withaqueous solution before charging, it is very difficult to mix thefeedstock with the catalyst before entering the system. According to thepresent invention, the catalyst is injected directly into feedstockline, as shown in FIG. 2. The hot heavy oil and residuum comes fromupstream device via line 4. The catalyst is injected by pump 3 via adistributor 5 into the heavy oil and residuum, and mixed with the heavyoil and residuum while flowing. High pressure hydrogen is introduced byline 6 into heavy oil and residuum. The mixture is passed by line 7 intoheater 8. The mixture which has been heated to reaction temperature isintroduced into reactor 10 by line 9. The hydrogenation reaction isperformed at 380-460° C. under 8-17 MPa. The reaction product is passedby line 11 to high-pressure separator 12, the gases separated are passedby line 17 to gas recovery and separating system 18. Hydrogen is washed,purified and recycled to the reactor by line 19. Lighter oil iswithdrawn by line 20. The liquid material separated from high-pressureseparator 12 is passed by line 13 to a solid separation device 14.Solids can be separated by a filtration or centrifugal separator. Theliquid product from which the catalyst powder and coke formed have beenremoved is withdrawn by line 16. The solid material filtrated may berecycled to a reactor or metal recycling system.

If sulfur content in the heavy oil and residuum feedstock is notparticularly high (for example, below 2.0 wt %) the prevulcanizing stepusing vulcanizing agent can be omitted. Generally, the sulfur content ofheavy oil and residuum needed to be hydrogenated is higher than 2.0 wt%.

Compared with the prior art, the present invention has the followingadvantages:

(1) Element nickel introduced into P and Mo water-soluble catalystsystem can effectively restrain coking;

(2) The distribution of products may be controlled by adjusting theMo/Ni atomic ratio in the catalyst in the reaction, thereby the productscheme can be changed flexibly to meet the market demand and therequirement of upstream and downstream flows;

(3) The total metal concentration in the aqueous solution may be up to16 wt %. When the amount of metals added in the catalyst is constant,less water is introduced into feedstock, therefore, the dehydrationstep, a very difficult step, may be omitted, while coke yield can becontrolled below 1.0 wt %;

(4) The prevulcanizing step using vulcanizing agent may be omitted.

EXAMPLES Examples 1-8

These tests are to examine the effect of added nickel on hydrogenationprocess of heavy oil and residuum.

To a vessel, metered amounts of commercial molybdenum oxide (orphosphomolybdic acid), phosphoric acid, and basic nickel carbonate wereadded, then a proper amount of deionized water was added, the mixturewas refluxed for 2 hours, there obtained was an aqueous catalystsolution containing Mo, Ni and P, the contents of which are shown inTable 1, wherein molybdenum oxide was replaced by phosphomolybdic acidin examples 2, 5 and 7.

A 750 ml high pressure reactor equipped with a stirrer was charged with250 g of Gudao Vacuum residuum (obtained from Shengli Refinary, CHINA),then an amount of the catalyst, the compositions of which are shown inTable 1, was added to provide a total amount of 200 ppm metals, based onthe amount of heavy oil and residuum feedstock. The reactor was sealed,flushed with hydrogen, fed with hydrogen to 7 MPa of hydrogen pressureat room temperature, heated with stirring at 440° C. for 1 hour. Thereaction product was analyzed for coke yield, yield of fraction below350° C. (AGO) and yield of fraction between 350-500° C. (VGO), theresults are shown in Table 1.

                                      TABLE 1                                     __________________________________________________________________________    Effects of catalyst in which Mo, Ni and P are in variant ratios on            catalyst performance in hydrocracking test                                    Examples 1  2  3  4   5   6  7   8                                            __________________________________________________________________________    Mo (wt %)                                                                              5.6                                                                              5.6                                                                              5.6                                                                              10  10  10 10  10                                           Ni (wt %)                                                                              0  0.2                                                                              0.4                                                                              0   0.6 0.8                                                                              0.9 1.0                                          P/Mo     0.15                                                                             0.15                                                                             0.15                                                                             0.087                                                                             0.087                                                                             0.10                                                                             0.087                                                                             0.087                                        Coke yield (wt %)                                                                      1.69                                                                             0.67                                                                             0.10                                                                             8.27                                                                              4.65                                                                              3.11                                                                             1.18                                                                              0.50                                         AGO (wt %)                                                                             32.69                                                                            32.60                                                                            32.54                                                                            45.54                                                                             42.29                                                                             41.21                                                                            40.16                                                                             40..13                                       VGO (wt %)                                                                             31.34                                                                            31.95                                                                            32.34                                                                            25.66                                                                             29.33                                                                             30.55                                                                            31.22                                                                             31.78                                        __________________________________________________________________________

The results of the tests illustrate that the catalyst in which nickelhas been added can effectively decrease coke yield in the process. Inaddition, even when P/Mo atomic ratio is only 0.087 (P/Mo atomic ratiois 0.087-0.10 in commercial phosphomolybdic acid) and content of Mo isup to 10 wt %, the coke yield can be controlled below 1 wt % in theprocess, if the nickel content is properly adjusted.

Examples 9-18

These tests show that the distribution of products may be adjusted in alarge scope by properly adjusting the compositions of the catalyst andother reaction conditions. Thus, the process has high flexibility. Theprocedures were the same as the above examples except that differentcompositions of the catalyst and different reaction conditions wereused. The results are shown in Table 2.

                                      TABLE 2                                     __________________________________________________________________________    Examples 9   10   11  12  13  14  15  16  17  18                              __________________________________________________________________________    Compositions of the                                                           catalyst                                                                      Mo (wt %)                                                                              5.6 4.0  4.9 4.9 3.5 2.0 8.0 6.4 6.6 7.0                             Ni (wt %)                                                                              0.7 0.3  0.4 1   1   0.1 0.8 1.0 0.8 1.1                             P/Mo     0.087                                                                             0.087                                                                              0.087                                                                             0.087                                                                             0.087                                                                             0.087                                                                             0.087                                                                             0.087                                                                             0.21                                                                              0.21                            Reaction conditions                                                           Reaction 430 440  450 390 430 440 430 430 435 435                             temperature, ° C.                                                      Reaction time, h                                                                       1   1    1   2   2   3   1   2   1   1                               Catalyst, ppm                                                                          160 1450 250 300 250 427 250 250 300 300                             Results                                                                       Coke yield (wt %)                                                                      0.02                                                                              0.446                                                                              0.94                                                                              0.03                                                                              0.27                                                                              0.98                                                                              0.1 0.67                                                                              0.08                                                                              0.02                            AGO (wt %)                                                                             33.0                                                                              30.1 47.3                                                                              16.1                                                                              36.8                                                                              40.8                                                                              35.5                                                                              37.6                                                                              36.4                                                                              38.3                            VGO (wt %)                                                                             31.2                                                                              36.3 28.0                                                                              18.0                                                                              43.9                                                                              45.1                                                                              29.9                                                                              39.6                                                                              38.1                                                                              39.2                            __________________________________________________________________________

It can be seen from the above examples that the distribution of productsmay be changed in a wide scope by adjusting the metal concentrations,element ratios in the catalyst and other reaction conditions. Light oilyield may be changed between 60% and 80%, and coke yield can becontrolled at less than 1.0 wt %.

Examples 19-24

These examples show the suspension bed hydrocracking reaction of heavyoil and residuum in a continuous laboratory apparatus.

The continuous suspension bed laboratory apparatus for hydrocracking ofheavy oil and residuum is shown in FIG. 1. Reffering to FIG. 1, a heavyoil and residuum feedstock and the catalyst aqueous solution were mixedin a mixing device 3. The mixed feedstock was passed by line 4, pump 5and line 7 to heater 8. Hydrogen was introduced into the system by line6. The feedstock was heated to 360-390° C. in a heating oven, and thenpassed by line 9 to reactor 10. The reaction products were passed byline 11 into high-pressure separator 12. The gases separated are passedby line 17 to gas recovery and separating system 18. Hydrogen waswashed, purified and recycled to the reactor by line 19. Lighter oil waswithdrawn by line 20. The liquid material separated from high-pressureseparator was passed by line 13 to a solid separation device 14. Theliquid product from which catalyst powder and few coke formed had beenremoved was withdrawn by line 16. The solid material filtrated may berecycled to a reactor or metal recycling system. The condition ofoperation and reaction results are shown in Table 3.

                                      TABLE 3                                     __________________________________________________________________________    Examples    19  20  21   22  23  24                                           __________________________________________________________________________    Compositions of catalyst                                                      Mo (wt %)   5.2 5.2 10.0 14.0                                                                              5.28                                                                              5.28                                         Ni (wt %)   0   0   0.8  1.0 0.4 0.4                                          P/Mo        0.087                                                                             0.087                                                                             0.087                                                                              0.087                                                                             0.087                                                                             0.087                                        Reaction conditions                                                           Reaction pressure (MPa)                                                                   14  14  14   14  14  14                                           Space velocity (h.sup.-1)                                                                 1   1   1    1   1                                                Temperature (° C.)                                                                 430 440 395  455 440 420                                          The amount of metal added                                                                 450 450 400  400 450 400                                          (ppm)                                                                         Coke yield (wt %)                                                                         1.5 2.2 0.25 1.0 0.72                                                                              0.21                                         AGO (wt %)  31.5                                                                              34.1                                                                              20.1 37.1                                                                              36.0                                                                              33.2                                         VGO (wt %)  29.5                                                                              30.2                                                                              22.5 33.2                                                                              32.8                                                                              28.3                                         __________________________________________________________________________

Examples 25-28

These examples show the results when the temperature of the feedstock ishigh and it is not suitable for mixing with the catalyst beforecharging. When the temperature of feedstock is high (for example theheavy oil and residuum directly comes from upstream device), it is verydifficult to mix the catalyst with the feedstock before entering thesystem. In this case, the hydrocracking process of the present inventioncan be performed by injecting the catalyst directly into feedstock line,the flow chart of which is shown in FIG. 2.

Reffering to FIG. 2, the hot heavy oil and residuum coming from upstreamapparatus was introduced by line 4. The catalyst aqueous solution wasinjected into residuum by pump 3 via a distributor. The heavy oil andresiduum was mixed with the catalyst while flowing. High pressurehydrogen was introduced by line 6, mixed with heavy oil and residuumfeedstock and was passed by line 7 to heater 8. The feedstock heated toreaction temperature was passed by line 9 into reactor 10. hydrogenationreaction was performed at 380-460° C. under 8-17 MPa. The reactionproduct was passed by line 11 to high-pressure separator 12. Thefollowing procedures were the same as that in examples 17-22. Theresults are shown in Table 4.

                  TABLE 4                                                         ______________________________________                                        Examples      25       26      27     28                                      ______________________________________                                        Mo (wt %)     5.2      5.28    10.0   10.0                                    Ni (wt %)     0        0.4     0.8    0.8                                     P/Mo          0.087    0.087   0.087  0.087                                   Reaction conditions                                                           Reaction pressure (MPa)                                                                     14       14      14     14                                      Space velocity (h.sup.-1)                                                                   1        1       1      1                                       Temperature (° C.)                                                                   430      440     410    440                                     The amount of metal added                                                                   450      350     250    300                                     (ppm)                                                                         Coke yield (wt %)                                                                           1.6      0.57    0.30   0.49                                    AGO (wt %)    32.6     36.5    31.8   40.8                                    VGO (wt %)    31.7     33.2    34.6   31.9                                    ______________________________________                                    

Although particular embodiments of the invention have been described andillustrated herein, it is recognized that modifications and variationsmay readily occur to those skilled in the art, and consequently it isintended that the claims be interpreted to cover such modifications andequivalents.

What is claimed is:
 1. A suspension bed hydrocracking process forcatalytic hydrocracking of heavy oil and residuum, comprising mixing aheavy oil and residuum feedstock with a catalyst, heating the resultingmixture and introducing it into a suspension bed reactor, and performingthe hydrocracking reaction at a temperature of 380 to 460° C. under ahydrogen pressure of 10 to 15 MPa; wherein said catalyst is adispersing-type, non-supported catalyst in the form of an aqueoussolution, comprises 2 to 15 wt % Mo, 0.1 to 2 wt % Ni and 0.1 to 3 wt %P, and is added in an amount to provide 150-1500 ppm active metals. 2.The suspension bed hydrocracking process according to claim 1, whereinsaid catalyst comprises 5 to 10 wt % Mo, 0.1 to 1.0 wt % Ni and 0.2 to 1wt % P.
 3. The suspension bed hydrocracking process according to claim1, wherein said catalyst comprises 6 to 8 wt % Mo, 0.3 to 0.8 wt % Niand 0.2 to 0.4 wt % P.
 4. The suspension bed hydrocracking processaccording to claim 1, wherein the heavy oil and residuum feedstock ismixed directly with the catalyst, and the resulting mixture isintroduced into a reaction zone to perform the hydrocracking reaction.5. The suspension bed hydrocracking process according to claim 1,wherein the feedstock is mixed directly with the catalyst, then mixedwith the hydrogen, and the resulting mixture is heated in a heating ovenand then enters the reactor.
 6. The suspension bed hydrocracking processaccording to claim 1, wherein the feedstock comes from an upstreamdevice and has a higher temperature, and the catalyst is injected intothe hot oil line by a pump via a distributor, then the resulting mixtureis introduced into the reaction system.
 7. The suspension bedhydrocracking process according to claim 1, wherein the feedstock isabout 100° C. and has such a high viscosity that it is not suitable formixing with the catalyst directly, the catalyst is first premixed with aamount of heavy oil and residuum having low viscosity with respect tothe feedstock, and then mixed with the feedstock having high viscosity,or added into the feedstock having high viscosity by a distributor. 8.The suspension bed by hydrocracking process according to claim 1,wherein the catalyst is added to provide 200 to 1000 ppm active metals.